WO1994027098A1 - Appareil et procedes de transfert thermique perfectionnes pour des systemes de sorption de solide-vapeur - Google Patents

Appareil et procedes de transfert thermique perfectionnes pour des systemes de sorption de solide-vapeur Download PDF

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Publication number
WO1994027098A1
WO1994027098A1 PCT/US1994/004343 US9404343W WO9427098A1 WO 1994027098 A1 WO1994027098 A1 WO 1994027098A1 US 9404343 W US9404343 W US 9404343W WO 9427098 A1 WO9427098 A1 WO 9427098A1
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WIPO (PCT)
Prior art keywords
refrigerant
heat transfer
reactor
transfer fluid
liquid
Prior art date
Application number
PCT/US1994/004343
Other languages
English (en)
Inventor
Lance D. Kirol
Uwe Rockenfeller
Original Assignee
Rocky Research
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Filing date
Publication date
Application filed by Rocky Research filed Critical Rocky Research
Priority to RU95120603A priority Critical patent/RU2142101C1/ru
Priority to DE69420404T priority patent/DE69420404T2/de
Priority to EP94914851A priority patent/EP0697085B1/fr
Priority to BR9406573A priority patent/BR9406573A/pt
Priority to JP52544594A priority patent/JP3391795B2/ja
Priority to CA002160659A priority patent/CA2160659C/fr
Priority to AU67090/94A priority patent/AU6709094A/en
Priority to HU9503185A priority patent/HU219393B/hu
Publication of WO1994027098A1 publication Critical patent/WO1994027098A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B17/00—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption type
    • F25B17/08—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption type the absorbent or adsorbent being a solid, e.g. salt
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B17/00—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption type
    • F25B17/08—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption type the absorbent or adsorbent being a solid, e.g. salt
    • F25B17/083—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption type the absorbent or adsorbent being a solid, e.g. salt with two or more boiler-sorbers operating alternately
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D20/00—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00
    • F28D20/003—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using thermochemical reactions
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A30/00—Adapting or protecting infrastructure or their operation
    • Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/62—Absorption based systems
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/14—Thermal energy storage

Definitions

  • Solid-vapor sorption systems such as those described in the aforesaid application, are used for cooling and refrigeration. These systems range from small devices having a cooling power of a few watts, to relatively large systems producing megawatts of cooling.
  • the larger systems lor example used in commercial HVAC applications, are usually designed to reject heat by using heat transfer fluids directed to air coils, air-cooled condensers, evaporative condensers, cooling towers, or to ground or surface water.
  • Pumped loops for transferring sorber heat to such heat rejection means are well-known to those skilled in the art.
  • relatively small systems such as appliances disclosed in U.S. patent no. 5,161,389, and in apparatus for electronic cooling disclosed in U.S. Patent No. 5,271,239 the use of extra cooling loops, and/or pump loops for transferring sorber heat to heat rejection is not practical.
  • the sorber may be insulated or otherwise provided with means for minimizing the heat loss since any heat losses to the environment reduce overall system efficiency and increase size and capacity requirements of the heat source.
  • efficient heat removal from the sorber is necessary, and must be transferred from the sorber to a heat rejection component, or be rejected directly from the sorber itself. The problem is exacerbated by the fact that elevated desorption temperatures create sorber-to-ambient temperature differentials favoring heat losses precisely at the time when such heat loss is undesirable.
  • the systems include apparatus in which the system refrigerant is used as the heat transfer fluid for cooling an adsorbing reactor.
  • the systems of the invention include activation of a heat rejection loop for cooling an adsorbing reactor using displacement of the heat transfer fluid without requiring thermostat or solenoid valve control of the cooling loop.
  • Apparatus is also disclosed for transferring heat from a single heat source to either of two reactors to provide continuous refrigeration or cooling.
  • FIG. 1 schematically illustrates a solid-vapor sorption system incorporating a bubble-pump assisted thermosyphon for transferring sorption energy to a condenser;
  • Fig. 2 is an enlarged view showing a flexible bubble-pump connector
  • Fig. 3 illustrates a system incorporating a vapor pump comprising a heater and check valve
  • Fig. 4 illustrates a solid-vapor sorption system incorporating an ejector-pump assisted thermosyphon
  • Fig. 5 illustrates a sorption system using a pressure deactivated thermosyphon
  • Fig. 6 illustrates sorption system incorporating a pressure deactivated thermosyphon using refrigerant pressure operated valves
  • Fig. 7 illustrates sorption system using a pressure deactivated thermosyphon system incorporating separate circuits for condensing heat transfer fluid and the system refrigerant;
  • Fig. 8 illustrates a sorption system having pressure activated thermosyphon and using a single reflux type condenser for transfer of sorption energy
  • Fig. 9 shows a sorption system with a pressure activated thermosyphon incorporating separate condenser circuits for each reactor;
  • Fig. 10 shows a sorption system with a pressure activated thermosyphon incorporating separate heat transfer fluid and refrigerant condenser circuits
  • Fig. 11 shows a two-stage constant pressure engine staging system with a pressure activated thermosyphon on both stages
  • Fig. 12 shows a two-stage constant pressure engine staging system with first stage thermosyphon activated by second stage refrigerant pressure
  • Fig. 13 illustrates a periodic refrigeration system with a heat rejection thermosyphon deactivated by a valve and refrigerant pressure
  • Fig. 14 shows a three reactor system using mechanical pumps for activating phase change cooling
  • Fig. 15 illustrates a single-source means for heating a dual sorber system.
  • the systems and apparatus disclosed herein may be used for any solid-vapor sorption including the complex compound systems disclosed in the aforesaid applications, the disclosures thereof which are incorporated herein by reference.
  • the systems of the invention may also be used for other solid-gas adsorbents including metal hydrides, activated carbons, silica gel, zeolites, carbonates, oxides, etc., and may be used for adsorbing any suitable refrigerant-gaseous reactants such as hydrogen, methane, ethane, helium, HFCs and HCFCs.
  • the systems herein are especially suitable for complex compound sorber systems of the aforesaid type for adsorbing polar refrigerants such as ammonia, water, methanol, alkanolamines, alkylamines, sulfur dioxide and phosphine on solid metal salts.
  • polar refrigerants such as ammonia, water, methanol, alkanolamines, alkylamines, sulfur dioxide and phosphine on solid metal salts.
  • Such complex compound reactor systems are especially useful in the design of small, compact devices operating at high power densities as described in U.S. application serial no. 07/931,036, filed August 14, 1992 and 07/975,973 filed November 13, 1992, and specifically using the complex compounds having increased reaction rates formed by restricting the volumetric expansion thereof during adsorption of the polar refrigerant on the metal salt as disclosed therein.
  • the systems and methods of the present invention preferably incorporate and use reactors containing a complex compound of one of the aforesaid polar refrigerants, and particularly preferred ammonia, adsorbed on a metal salt comprising a halide, nitrate, nitrite, oxalate, sulfate, or sulfite of an alkali metal, alkaline earth metal, transition metal, zinc, cadmium, tin, aluminum, sodium boroflouride, or double metal chloride, and in which the volumetric expansion of the complex compound is limited or restricted during at least the initial adsorption reaction to form at least a partially coherent, cohesive, physically self-supporting reaction product capable of increased chemisorption reaction rates as compared to a complex compound formed without so limiting the volumetric expansion.
  • a complex compound of one of the aforesaid polar refrigerants, and particularly preferred ammonia adsorbed on a metal salt comprising a halide, nitrate, n
  • These salts may also be mixed with a zeolite, activated carbon, activated alumina or silica gel prior to the initial ammonia adsorption.
  • Preparation of the aforesaid preferred compounds used in the reactors of apparatus and systems of the present invention are capable of achieving maximum power density per mass of adsorbent, maximum power density per mass of reactor and maximum power density per desired or needed reactor volume.
  • Half cycle times i.e., adsorption or desorption reaction times of the reactions having such improved reaction rates are carried out in less than 30 minutes, preferably in less than about 20 minutes and typically between about 3 and about 15 minutes.
  • adsorption is intended to cover any such solid-vapor sorption reactions, regardless of whether it is termed adsorption or absorption.
  • the basic solid-vapor sorption systems used herein are schematically illustrated in Figs. 1 - 10 incorporating two sorbers, also referred to herein as reactors, one of which is adsorbing while the other is desorbing.
  • the adsorbing reactor or sorber to be adsorbed is cooled to near ambient temperature to lower the vapor pressure of the absorbent therein. As the cooled adsorbent vapor pressure drops below the evaporator pressure the sorber draws refrigerant vapor from the evaporator. This flow of refrigerant from the evaporator provides the refrigeration or cooling effect of the system.
  • the control of the flow of refrigerant to and from the adsorbing reactor may be passive, for example, using check valves or back-pressure control valves, or the flow may be actively controlled, using for example, solenoid valves, or motor or pressure operated valves.
  • Heat created during the exothermic adsorption reaction is removed to maintain the sorber at the proper adsorption temperature. While the adsorbing reactor is cooled to initiate adsorption, the other sorber is heated until the vapor of the adsorbent therein is greater than the condenser pressure, at which time refrigerant desorption to the condenser begins. Heat supplied to the desorption reactor provides the necessary energy required to drive the endothermic desorption and to overcome heat loss in the system. At the end of one sorption half-cycle or phase, the roles of the two sorbers are reversed.
  • the systems schematically illustrated in Figs. 1 - 14 illustrate the invention of an apparatus and method of rejecting the heat of adsorption created in a reactor during adsorption.
  • the systems utilize a heat transfer fluid having a phase change from liquid to gas at or below the temperature of the adsorbing reactor.
  • the heat transfer fluid which may be liquid or a mixture of liquid phase and gaseous phase, is directed to the adsorbing reactor and is exposed in heat exchange communication with the adsorbent during the exothermic adsorption reaction.
  • the heat from the exothermic reaction is transferred to the heat transfer fluid thereby vaporizing at least a portion of the liquid phase thereof and rejecting the heat.
  • thermosyphon heat transfer loop which provides or assists in circulation of the heat transfer fluid from the adsorbing reactor to the condenser.
  • thermosyphon is intended to include any loop or system in which reactor cooling results from phase change of liquid heat transfer fluid or refrigerant, the condensate of which is returned to system liquid level by gravity.
  • the systems may be designed to use the system refrigerant as the heat transfer fluid, or for use of different, separate compositions.
  • the sorbers or reactors may incorporate internal and/or external heat transfer surfaces.
  • the condensers may incorporate natural or forced (fan) convective cooling.
  • Different types of expansion devices such as a capillary tube, expansion valve, orifices, porous media, etc. may be used on the evaporator inlet.
  • the check valves or one- way valves may be replaced by active control valves, such as solenoids.
  • the heater elements for driving the desorption reaction may be mounted on heat-transfer surfaces, as illustrated or embedded in the sorbers.
  • Heating means may comprise electrical resistance wires or heaters, or use heat transfer liquids or hot water or steam tubes or flue-gas tubes for directing hot gases of combustion, radiant heating, or any other suitable method of thermal conductance.
  • Heating means may comprise electrical resistance wires or heaters, or use heat transfer liquids or hot water or steam tubes or flue-gas tubes for directing hot gases of combustion, radiant heating, or any other suitable method of thermal conductance.
  • Fig. 1 there is illustrated a solid-vapor adsorption system.
  • the system is shown in the half-cycle during which reactor 10 is desorbing while reactor 20 is adsorbing.
  • Desorbing reactor 10 is heated by energized heating elements 13 to provide the necessary heat for driving the endothermic desorption reaction as previously described.
  • the heat transfer surface of adsorption reactor 20 communicates with condenser 12 via conduits 40 and 41.
  • the refrigerant is used as the gaseous reactant which is adsorbed and desorbed on the solid adsorbent, and as the heat transfer fluid for cooling the adsorbing reactor.
  • the arrows in the various conduits are shown in the direction of refrigerant flow during the aforesaid half-cycle.
  • the clear or white centered arrows illustrate vapor refrigerant flow
  • the hatched arrows show a two-phase refrigerant flow
  • the solid dark centered arrows indicate liquid refrigerant flow. Piping below the sorbers is filled with liquid refrigerant approximately to level 99.
  • the sorbent With heater element 13 in sorber 10 energized, the sorbent is heated until its vapor pressure is greater than the pressure in condenser 12. At that time, refrigerant vapor flows from sorber 10 through pipe 23 and check valve 37 to vertical tube 22 which is connected to the heat transfer tube 17 in sorber 20. Vapor flowing into the vertical tube 22 creates a "bubble-pump" effect and lifts liquid refrigerant standing in the tube to the heat transfer surfaces of heat transfer tube 17. Thus, the heat transfer liquid directed into reactor 20 is a mixture of liquid and vapor phase refrigerant.
  • the liquid refrigerant vaporizes on the reactor heat transfer surfaces, completely or partially, it cools reactor 20 to near condenser temperature, and adsorption of the refrigerant on the sorbent begins. Heat generated by the exothermic adsorption reaction is removed by the vaporizing refrigerant, and the sorber is maintained within a few degrees of condenser temperature.
  • the two-phase refrigerant mixture leaving reactor 20 is directed to separator 39, typically a tee in the tubing, with the vapor portion of the refrigerant directed to the condenser 12 via pipe 41, and liquid refrigerant portion returned to the tubing below the sorbers via line 42.
  • Vaporized refrigerant is condensed in condenser 12 and returned to the liquid in the lower tubing via pipe 21.
  • Liquid refrigerant in the lower tubing 44 is also directed via pipe 26 through expansion valve 35, to feed the evaporator 14.
  • Gaseous refrigerant from the evaporator is directed via pipe 24 into the adsorbing reactor.
  • One way valves 31 and 33 direct refrigerant to a reactor during the adsorption reaction phase.
  • Bubble pumps often referred to as gas-lift pumps, used to provide condensed coolant to adsorbing reactor can be driven by vapor desorbed from the opposing reactor, as described above and illustrated in Fig. 1, or can be driven by a heater, typically electrical, on the vertical riser of the pump. The heater must be located on a vertical or nearly vertical tube or pipe and below the liquid level.
  • Such a heater located on a liquid refrigerant line generates vapor thus reducing density of the coolant in the vertical riser relative to liquid standing in the rest of the system.
  • the reduced density coolant and vapor flow upward creating a pumping action.
  • the advantage of using a heater instead of desorbed vapor for activation of the bubble pump is that it allows cooldown and adsorption of the reactor to begin before the opposing reactor is heated to desorption temperature and pressure. This advantage results in reduced total time for heatup and cooldown and an overall increase in the cooling power of the system.
  • a vapor pump in which a heater generates vapor in a tube of liquid heat transfer fluid or refrigerant and a check valve prevents backflow toward the system liquid reservoir, thus forcing coolant flow toward the adsorbing reactor heat transfer surface.
  • the check valve With the check valve, the heater need not be in the vertical riser, orientation sensitivity is greatly reduced and less liquid head is required to feed the pump.
  • Such a feature is illustrated in Fig. 3, with heaters 47 and 49 positioned downstream from check valves 11 and 13 along the conduits from liquid reservoir 71.
  • the system illustrated in Fig. 1 may be sensitive to orientation, because the bubble pump vapor feed must be somewhat submerged below the liquid refrigerant level, whereas the inlet to the sorber heat exchange surface at the bubble pump exit must not be submerged.
  • orientation sensitivity may be substantially reduced by connecting the bubble pump on a pivot or flexible connector as illustrated in Fig. 2.
  • the bubble pump 15 is provided with a pair of flexible or pivoting connectors 19 and 29 along pipes 23 and 22, respectively, which allow the lower portion of the connected pipes, below the connectors, to hang vertically into receiver 27, below liquid level 99.
  • Fig. 4 illustrates a solid-vapor adsorption system of substantially the same design shown in Fig. 1, but incorporating an ejector for delivering cooling liquid to the adsorber reactor.
  • ejectors 51 and 53 sometimes referred to as injectors, convert kinetic energy of the vapor refrigerant stream to a pressure head for pumping liquid refrigerant to a reactor.
  • Advantages of ejectors over the bubble pump include reduced sensitivity to orientation by using a liquid reservoir 50, preferably having a conical or spherical bottom, or a tall cylindrical reservoir in which the ejectors are submerged at any desired inclination, more robust pumping, and delivery of liquid instead of two-phase mixture to the sorber to be cooled.
  • a pivoting or flexible downcomer cooperating with the ejector at the bottom of the reservoir may also be used to further reduce orientation sensitivity.
  • Figs. 5, 6 and 7 illustrate sorption systems using a phase change thermosyphon loop for cooling either sorber.
  • the thermosyphon loop on the sorber being desorbed is deactivated by pressure generated inside the sorber. Deactivation is accomplished by forcing all of the liquid heat transfer fluid out of the thermosyphon loop.
  • the system refrigerant is also the heat transfer fluid, while in Fig. 7, the system uses different refrigerant and heat transfer fluid compositions.
  • Fig. 5 the schematic system shown is a pressure deactivated thermosyphon for transferring energy to the condenser.
  • sorber 10 is desorbing with heater element 13 energized, and sorber 20 is adsorbing with its heater deenergized.
  • Valves 63 and 66 are actively controlled. With valve 63 closed, the heat transfer tubes 16 in reactor 10 do not communicate with the condenser 12 whereby pressure generated by heat forces liquid refrigerant out of the heat transfer tube, through conduit 77, and into the heat transfer tubes of reactor 20.
  • Initial pressure to deactivate the thermosyphon circuit is provided by the reactor heaters or by auxiliary heaters located in the thermosyphon loop which may be activated just long enough to increase vapor pressure in the loop sufficient to initiate deactivation. However, once desorption begins, pressure of the desorbed vapor maintains the circuit deactivated thereby minimizing heater energy consumed to maintain pressure in the heat transfer tube. With valve 66 open, the refrigerant may pass through the reactor 20 to the condenser and vaporization of liquid refrigerant in reactor 20 cools it to adsorption temperature whereby adsorption therein begins. Refrigerant vaporization then continues to remove heat of adsorption.
  • open valve 66 activates a phase change thermosyphon heat transfer loop between reactor 20 and the condenser, while closed valve 63 deactivates the thermosyphon loop on the desorbing reactor 10 due to the pressure generated therein as previously described.
  • valve 66 is closed, the heater in reactor 10 is deenergized and valve 63 is opened.
  • refrigerant flow is controlled by valves 31, 33, 62 and 65. These valves may be one-way check valves, or may be actively operated.
  • the actively operated or actuated valves 63 and 66 may be solenoid valves, sequenced with the same control circuits used to energize and deenergize the heaters.
  • the actively controlled valves may be piston operated valves driven by air pressure or by refrigerant vapor pressure generated in the desorbing reactor.
  • FIG. 6 Another variation of a pressure deactivated thermosyphon system is illustrated in Fig. 6.
  • the system shown uses 3-way valves 72 and 73 controlled by pressure in the communicating sorber.
  • Valves 72 and 73 are spring-operated, 3-port valves communicating between the respective sorbers and condenser 12. When the sorber pressure is less than or equal to the condenser pressure, valve plug 79 is urged to a position to close communication between the desorbing refrigerant outlet pipe and the condenser and to open the sorber heat transfer circuit to the condenser.
  • Valve 73 is shown in that position.
  • the rising reactor pressure forces the valve plug in the opposite direction, closing heat transfer circuit communication with the condenser, and directing desorbing refrigerant to force liquid refrigerant from the reactor heat transfer tube 16 to reactor 20 heat transfer tube 17 via conduit 77.
  • the actuated valves which communicate between the respective reactors and the condenser are preferably operated so that direct communication between a reactor and the condenser is closed as soon as the heater in the desorbing reactor is energized. Such operation ensures that liquid refrigerant in a reactor heat transfer tube is not evaporated prior to the valve closing and forcing refrigerant from the tube.
  • an electrically actuated valve which can be closed at precisely the desired time is preferred.
  • the desirability of such timing is to minimize energy consumption.
  • the apparatus shown in Figs. 5 and 6 may be modified for routing desorbed refrigerant vapor directly to the condenser, without passing through the reactor heat transfer section.
  • conduits 61 and 64 would communicate with conduit 59 above, or upstream from valves 63 and 66, respectively.
  • One-way valves 62 and 65 could be replaced by using thermostatically operated valves with a sensor connected to the reactor heater for directing the desorbed refrigerant to condenser 12.
  • a solenoid valve could be used for the same purpose.
  • the apparatus of Fig. 6 could be similarly modified.
  • the pressure deactivated thermosyphon system utilizes separate refrigerant and coolant (heat transfer fluid) condensers and associated fluid loops.
  • refrigerant and coolant heat transfer fluid
  • Such system design may be preferred over the previously described systems using a single composition for both the cooling fluid and the system refrigerant and requiring only a single condenser , where it is desirable to minimize the refrigerant inventory, to allow use of a heat transfer fluid having improved heat transfer properties, or to allow the use of different pressures in the heat transfer components of the system.
  • useful heat transfer fluids for such systems include water, alcohols, light hydrocarbons, heat transfer oils, and DOWTHER ® phase change heat transfer media.
  • valves 60 and 67 are closed to deactivate the thermosyphon of their respective sorbers during desorption.
  • Valves 60 and 67 may be operated electrically, thermostatically, or using pressure activation.
  • the valve communicating the desorbing reactor with the coolant condenser 12 be closed prior to energizing the desorption reaction heater in order to minimize heat losses through the vaporizing coolant. Electrically or thermostatically operated valves are preferred for such a purpose.
  • thermosyphon loop Auxiliary heaters may be provided in the thermosyphon loop and energized just long enough to deactivate the loop until the pressure from desorption reactor heating creates sufficient vapor pressure to take over.
  • a separate condenser 55 is used for condensing desorbed refrigerant vapor from a desorbing reactor.
  • the condensed refrigerant is directed through conduit 58 and expansion valve 35 to evaporator 14, while condensed coolant is directed to the adsorbing reactor via conduit 21.
  • Vaporized refrigerant is directed via conduit 24, valve 33 through conduit 46 to adsorbing reactor 20 in the half-cycle illustrated. Again, at the end of the described process, the functions of the two sorbers are reversed.
  • the approximate coolant (heat transfer fluid) fill level 99 is also shown.
  • thermosyphons using a pressure activated thermosyphon are shown in which desorption pressure activates a heat transfer loop, in contrast to the pressure deactivated thermosyphon systems illustrated in Figs. 5 - 7.
  • the pressure activated thermosyphons provide activation of heat transfer between sorbers, i.e., one sorber activates heat rejection in the other sorber. .An advantage of such a system is the reduction or elimination of timing difficulties caused by heat transfer deactivation and elimination of the loss of heater energy due to refrigerant evaporation prior to deactivation of heat transfer loop.
  • the pressure activated thermosyphon system illustrated in Fig. 8 incorporates a reflux type condenser 70 for condensing the refrigerant which is also the coolant or heat transfer fluid.
  • reactor 90 is desorbing with vaporized refrigerant directed therefrom through one-way valve 91 and conduit 96, through reservoir 85 and into the heat transfer surface of adsorbing reactor 80 via conduit 97.
  • the pressure from the desorbing reactor and the desorbed refrigerant forces liquid refrigerant from reservoir 85 into the heat transfer surface 48 of reactor 80, where it vaporizes and cools the reactor for removing heat of absorption.
  • Refrigerant vapor condensed in condenser 70 returns to reactor 80 for continuous cooling.
  • Heating elements 92 and 98 are shown in the respective reactors, as is the liquid level 99 for the half-cycle illustrated.
  • a capillary tube 83 or equivalent expansion device directs liquid refrigerant to evaporator 14 for expansion and direction to the adsorbing reactor via conduit 87.
  • An alternative to a single reflux type condenser system shown in Fig. 8 may utilize separate return legs for condensed refrigerant and for providing a thermosyphon. Such an embodiment is illustrated in Fig. 9, with reactor 90 desorbing refrigerant, and reactor 80 adsorbing in the half-cycle shown.
  • the liquid refrigerant directed into adsorbing reactor 80 is vaporized by heat transfer along the heat transfer surfaces of heat transfer section 48, with the vaporized refrigerant directed to condenser 95.
  • the system illustrated in Fig. 8 may also incorporate check valves and a single expansion device for feeding evaporator 14, as shown in Fig. 9, to prevent fluid migration between sides.
  • Yet another alternative is illustrated in Fig. 10 showing a system in which a coolant or heat transfer fluid other than the system refrigerant is used.
  • the pressure activated thermosyphon system incorporates diaphragms in the reservoirs which displace liquid coolant using pressure without mixing of the refrigerant and the coolant.
  • desorbed refrigerant is directed through conduit 108 into reservoir 101 where it forces diaphragm 116 to displace liquid coolant out of the lower cavity 117 and into adsorbing reactor 80 via conduit 114. Again, the vaporized liquid coolant is directed to the coolant condenser 95, and condensed liquid directed back to the reservoir 101.
  • Refrigerant adsorbed in adsorbing reactor 80 is directed thereto from evaporator 14, and a portion of the desorbed refrigerant from reactor 90 is split off from conduit 108 via conduit 115 and one-way valve 107 and conduit 109 to refrigerant condenser 110.
  • Other movable interface means may be substituted for the diaphragm shown. For example, bellows or pistons, etc., may be used at the liquid, gas interface for displacing liquid heat transfer fluid in response to gas pressure.
  • thermosyphon systems with system refrigerant the same or different than coolant, may also be activated with a small heater in the coolant reservoir.
  • small heaters 89 may be provided in reservoirs 85 and 86 of the systems shown in Figs. 8 and 9 to generate pressure and displace the coolant into the thermosyphon loop.
  • the advantage of using such heaters is that cooldown and adsorption can start before desorption pressure is generated in the opposing reactor, with the effect of shortening total cooldown/heatup time and increasing net system cooling capacity.
  • a heater and desorbing vapor may also be combined to provide timing advantages while minimizing energy consumption; once desorption pressure is generated in the opposing reactor, the heater may be deactivated.
  • thermosyphon heat transfer loops may be provided between reactors of adjacent higher and lower staged reactors.
  • three thermosyphon heat transfer loops may be used, one between the intermediate and highest stage reactors, one between the intermediate and lowest stage reactor, and one between the lowest stage reactor and the condenser.
  • the lower stage reactors serve the function of a "heatsink” or heat transfer fluid condenser, and the lowest stage reactor rejects heat to the condenser itself.
  • These thermosyphon loops use phase change heat transfer fluids in the thermosyphon heat transfer loops and may be provided with dual-circuit heat transfer conduits as disclosed in aforesaid U.S. application 07/931,036.
  • the lowest stage circuit may use the system refrigerant for heat transfer to the refrigerant condenser, or a different coolant and separate condenser.
  • the higher stage reactors usually use a coolant different from the system refrigerant unless a low pressure refrigerant such as water is used.
  • a two-stage discrete constant pressure staging system is shown .
  • the schematically illustrated system is similar in design to the systems illustrated in Figs. 7 and 8 incorporating pressure activated thermosyphon loops used on both stages.
  • reactors 110 and 120 are the lower stage (cooler) reactors and reactors 130 and 140 are the higher stage (hotter) reactors.
  • the higher stage reactors 130 and 140 use a coolant other than the refrigerant whereas the lower stage reactors 110 and 120 use system refrigerant as the coolant for rejecting heat to the condenser 121.
  • the lower stage sorbers may incorporate dual- circuit heat transfer section components such as illustrated and described in U.S. application serial no.
  • the heat transfer section 148 may be designed for heat transfer fluid condensation in a small tube 143 coiled inside of a larger tube 149 containing the heat rejection fluid, such as schematically illustrated in reactors 110 and 120.
  • the system illustrated in Fig. 11 shows a half-cycle with reactor 120 desorbing while reactor 140 is adsorbing refrigerant.
  • reactor 110 is adsorbing refrigerant while reactor 130 is desorbing.
  • Desorbing reactor 130 directs refrigerant vapor to reservoir 101 expanding diaphragm 116 and displacing the liquid heat transfer fluid therein.
  • the heat transfer fluid is shown stippled.
  • the liquid heat transfer fluid is directed into adsorbing reactor 140, where it is vaporized, cooling the reactor. From there the vaporized heat transfer fluid is directed to lower stage desorbing reactor 120 and is condensed at the lower temperature conditions therein.
  • the vaporized refrigerant desorbed in reactor 120 is directed through reservoir 138 and mixes with liquid condensed refrigerant in conduit 144. The mixture is then directed into reactor 110 by the activated thermosyphon loop created in heat transfer section 148 to provide heat transfer cooling.
  • refrigerant evaporator 125 provides vaporized refrigerant for adsorbing reactors.
  • thermosyphon loop heat transfer advantages of the invention may be used to take advantage of the thermosyphon loop heat transfer advantages of the invention.
  • the system illustrated in Fig. 12 shows an example of the control of a heat rejection thermosyphon loop using refrigerant pressure across stages in contrast to the use of two sorbers in each stage as previously illustrated.
  • refrigerant vapor from the second stage reactor 134 activates a heat rejection thermosyphon on first stage reactor 124 as adsorption occurs therein.
  • Control of heat transfer fluid 131 shown stippled in the heat transfer pipe extending between the two reactors is accomplished using valve 129, which may be externally activated, such as a solenoid valve.
  • a heat source 127 provides heat input to the heat transfer fluid for driving the desorption reactions of the system.
  • Cold fill levels 99 are shown for the system as is evaporator 122, expansion device 123 and refrigerant condenser 139.
  • Refrigerant vapor from the second stage reactor 134 activates the heat rejection thermosyphon of first stage reactor 124, which may incorporate a heat transfer section for cooling the reactor as previously described for lower stage reactors in Fig. 11.
  • Activation may be pressure driven, as shown, or flow driven, i.e., bubble pump or ejector, or driven by a mechanical pump. Arrows illustrating liquid, gaseous and mixed phase refrigerant are not shown.
  • Fig. 13 an embodiment illustrating periodic refrigeration systems is shown, which uses a single reactor or sorber.
  • a periodic single stage system features a thermosyphon loop for cooling the reactor during adsorption with valve 151 open to complete the heat rejecting thermosyphon loop to the condenser 153 and conduit 156 back to heat transfer section 160 of the reactor.
  • thermosyphon loop is activated.
  • thermosyphon During desorption, by closing valve 151 and energizing heater 158, the thermosyphon is deactivated, and increased vapor pressure in heat transfer section 160 of the reactor forces liquid refrigerant out of the heat transfer tubes and completely deactivates the thermosyphon to prevent heat rejection.
  • the system incorporates a reservoir 152 for liquid refrigerant, one way valves 157 and 159, evaporator 154, and expansion device 155.
  • the reservoir may include a heater which is activated for displacing refrigerant therefrom.
  • the reservoir may be replaced by a mechanical pump, or a vapor pump, assisted with a heater, and/or a check valve for driving liquid into the system. Again, arrows illustrating different refrigerant phases are not shown.
  • thermosyphon loops for heat rejection are activated by pumping means such as bubble pump, vapor pump, ejector, or by fluid displacement.
  • pumping means such as bubble pump, vapor pump, ejector, or by fluid displacement.
  • mechanical pumps may be used to activate phase-change thermosyphon systems for all of the above cycles by supplying a small amount of condensed coolant to the heat transfer surface.
  • Such use of a mechanical pump may result in increased power density with proper cycle timing because heatup and cooldown can proceed simultaneously, and because adsorption and desorption periods need not be of equal duration as is required by desorption-driven pumping systems.
  • Use of a mechanical pump also increases control options available. For example, when a thermostat indicates that cooling is no longer needed, the pump may be turned off and adsorption continued at a much lower rate to maintain load temperature without excessive cooling.
  • Thermostatic demand for more cooling causes the pump to be activated and sorption rates would increase. During periods of low demand, desorption of the opposing sorber may also proceed without affecting performance of the adsorption, thus charging the system for the next call for cooling.
  • three or more sorbers may be used to provide constant evaporator suction and reduce cycling losses due to refrigerant migration in the off periods or simply to provide backup or excess peak capacity. Such a system is illustrated in Fig. 14.
  • Pumps 136 provide liquid refrigerant to heat transfer sections 137 of reactors 142.
  • the system includes six check valves 133 along the gaseous refrigerant lines to and from the reactors, as shown.
  • FIG. 15 shows an alternative apparatus design utilizing a single heat source and a single valve cooperating with heat transfer loops for controlling and directing the flow of heated vapor or a mixture of vapor and liquid phase heat transfer fluid to the sorbers at the desired time in the reaction cycle.
  • a single heat source for example gas flame, solar concentrator, campfire, electric element, and the like, vaporizes a heat transfer fluid in boiler 175, with single valve 171 directing the vapor to either sorber 172 or 174, at the desired time. Condensation of the vapor in the sorber generates heat which may be transferred to the sorbent utilizing a dual circuit heat transfer system as previously described, or by condensing the vapor in a small condenser tube 177 in contact with the sorber heat transfer surface.
  • Condenser tube 177 may be straight as illustrated and bonded to one side of the heat transfer surface, or it may be coiled or concentric relative to the cooling channel of the heat transfer surface with axial fins connecting to the sorber as is commonly used in double- wall heat exchangers.
  • vaporized heat transfer fluid from boiler 175 is directed to valve 171, which is positioned to direct the vapor to reactor 174, where it is condensed thereby releasing heat to drive desorption in the reactor.
  • the condition of valve 171 is closed relative to reactor 172, in the adsorbing stage, and which may be cooled as previously described hereinabove.
  • Such a means for heating may be used as an alternative to the conventional use of resistive electrical heating for small or miniaturized sorption refrigerators or refrigeration systems.
  • systems of the invention disclosed herein are advantageous over prior art systems requiring the use of solenoid and/or thermostatically controlled components for operating and controlling the cooling loops for cooling adsorbing reactors. Instead, the systems of the present invention use vapor pumps, bubble pumps, mechanical pumps, or other vapor pressure displacement of the heat transfer fluid to activate the heat rejection loop. Moreover, systems of the present invention offer the advantage of using the system refrigerant as the heat transfer fluid in the thermosyphon cooling loop.
  • the systems described herein may be used in any solid-vapor sorption refrigeration systems and applications. The invention finds particular advantage for small or miniature refrigeration engines, for example 5 to 25 watts cooling capacity, such as personal refrigerators and freezers, having few moving parts, and manufactured at relatively low cos .
  • refrigerators, freezers, coolers and other appliances may incorporate and benefit from such inventions when incorporating such features of the invention, the resulting appliances will have substantially improved capacity including particularly noiseless and vibrationless operation while benefiting from reliable, simple, and inexpensive components, again due to the substantial reduction in the valves, pumps, and other power consuming components which are typically required in presently commercially available refrigerators, freezers, etc.
  • devices and appliances incorporating the components , methods and advantages of the present invention include small capacity refrigerators of between about 5 watts and 50 watts, and small capacity freezers of between about 5 watts and about 100 watts, having extreme temperature lifts.
  • High specific power density low wattage cooling appliances of up to about 300 watts capacity may be constructed of components incorporating the present invention.
  • Such small or personal refrigerator cooling around 0°C to about 8°C and freezers cooling at between about minus 30 and minus 10°C, and typically up to about 7 cubic feet are examples of such appliances.
  • Other specific examples include high power, rapid freezing devices, such as disclosed in U.S. Patent 5,161,389 or similar devices such as ice cream makers, ice cube makers, medical freezers and the like.
  • Yet other cooling devices include air conditioning equipment, especially small room air conditioners of less than about 1.5 ton capacity or automotive or personal cooling devices, and the like.
  • Other cooling apparatus which may be designed to incorporate the advantageous components and methods of the present invention include the electronic cooling systems disclosed in U.S. patent no.
  • a list of specific types and examples of apparatus and appliances include: consumer leisure appliances, up to about 70 watts capacity, such as small or portable or personal freezers, refrigerators or refrigerator/freezer combination units, refrigerator, freezer or combination appliances which may be installed in recreational vehicles, boats, automobiles or trucks, and mini-bar refrigerators, freezers or combination units; kitchen appliances, up to about 400 watts, such as rapid freezers, standing alone or combined with microwave and/or standard refrigerator/freezer units, iced tea/coffee makers, ice cube makers, ice cream makers, freeze dryer units, and drink or water coolers; display and vending equipment and apparatus, up to about
  • watts such as coolers, freezers and ice makers
  • durable good appliances up to about 400 watts such as household refrigerators and freezers and commercial freezers and refrigerators, with or without rapid freeze capability, and dehumidifiers
  • building air conditioning appliances including residential split unit air conditioners and heat pumps (IRT to 5RT) , light commercial split unit air conditioners and heat pumps (5RT to 20RT) , room air conditioners (1/2 RT to 1-1/2 RT) and residential dehumidifiers
  • electronic cooling apparatus up to about 200 watts, for electronic and chip cooling and electronics system box air conditioning
  • miscellaneous equipment and appliances such as HVAC products in excess of 20RT capacity, medical and laboratory appliances, military products including combat, pilot and astronaut suits, industrial and commercial heat

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Chemical & Material Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Sorption Type Refrigeration Machines (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Treating Waste Gases (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

Dans un système de réaction par sorption comportant un ou plusieurs premiers réacteurs (10) dans lesquels un réfrigérant est en alternance adsorbé et désorbé, ainsi qu'un ou plusieurs deuxièmes réacteurs (20) dans lesquels un réfrigérant est en alternance désorbé et adsorbé, respectivement, et possédant une boucle de refroidissement (16, 60, 68, 67, 56, 12, 21) pour diriger le fluide de transfert thermique à destination et en provenance desdits réacteurs (10, 20), un procédé de refroidissement d'un réacteur d'adsorption consiste à diriger le fluide de transfert thermique en phase liquide, subissant un changement de la phase liquide à la phase gazeuse à une température égale ou inférieure à la température d'adsorption, vers un réacteur d'adsorption, ledit fluide étant exposé, pour échange thermique, à l'adsorbant, à l'aide d'un fluide de transfert thermique vaporisé, pour véhiculer le fluide de transfert thermique liquide dans la boucle de refroidissement. Le réfrigérant peut servir de fluide de transfert thermique. L'invention décrit un appareil permettant la mise en ÷uvre du procédé.
PCT/US1994/004343 1993-05-11 1994-04-20 Appareil et procedes de transfert thermique perfectionnes pour des systemes de sorption de solide-vapeur WO1994027098A1 (fr)

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RU95120603A RU2142101C1 (ru) 1993-05-11 1994-04-20 Усовершенствованное устройство и способы теплопередачи в сорбционных системах твердое тело - пар
DE69420404T DE69420404T2 (de) 1993-05-11 1994-04-20 Wärmeübertragungsvorrichtung und verfahren für feststoff-dampf-sorptionsanlagen
EP94914851A EP0697085B1 (fr) 1993-05-11 1994-04-20 Appareil et procedes de transfert thermique perfectionnes pour des systemes de sorption de solide-vapeur
BR9406573A BR9406573A (pt) 1993-05-11 1994-04-20 Equipamento e processos aperfeiçoados para transferência de calor para sistemas de adsorção sólido-vapor
JP52544594A JP3391795B2 (ja) 1993-05-11 1994-04-20 固体蒸気収着システムのための改良された熱伝達装置および方法
CA002160659A CA2160659C (fr) 1993-05-11 1994-04-20 Dispositif ameliore d'echange thermique; methodes d'adsorption solide-vapeur
AU67090/94A AU6709094A (en) 1993-05-11 1994-04-20 Improved heat transfer apparatus and methods for solid-vapor sorption systems
HU9503185A HU219393B (en) 1993-05-11 1994-04-20 Method for cooling and cooling device

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US5954893A 1993-05-11 1993-05-11
US08/059,548 1993-05-11

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EP0702199A1 (fr) * 1994-09-19 1996-03-20 Nippondenso Co., Ltd. Appareil de refroidissement à adsorption
WO1996030706A1 (fr) * 1995-03-28 1996-10-03 Rocky Research Systemes ameliores de chauffage et de climatisation utilisant des reacteurs de sorption a vapeur solide capables de taux de reaction eleves
CN102155813A (zh) * 2011-04-20 2011-08-17 上海交通大学 空调机组冷凝热驱动的热化学吸附制冷装置
CN103615831A (zh) * 2013-11-15 2014-03-05 无锡雪浪环境科技股份有限公司 一种蒸汽压力升降吸附法及使用该方法的热泵
WO2017207262A1 (fr) * 2016-05-30 2017-12-07 Climatewell Ab Tube caloporteur hybride
US10006670B2 (en) 2013-05-02 2018-06-26 Carrier Corporation Method for managing a refrigerant charge in a multi-purpose HVAC system
US10240825B2 (en) 2013-11-13 2019-03-26 Mahle International Gmbh Evaporator set, preferably for a thermally driven adsorption device, and adsorption device

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DE10217443B4 (de) * 2002-04-18 2004-07-08 Sortech Ag Feststoff-Sorptionswärmepumpe
CN1306239C (zh) * 2004-10-14 2007-03-21 上海交通大学 太阳能吸附中央空调冷却塔
EP2568792A1 (fr) * 2011-09-06 2013-03-13 ABB Research Ltd. Appareil
JP2013094722A (ja) * 2011-10-31 2013-05-20 Denso Corp 反応器
WO2013169774A2 (fr) 2012-05-07 2013-11-14 Phononic Devices, Inc. Composant d'échangeur de chaleur thermoélectrique comprenant un couvercle d'étalement de la chaleur protecteur et une résistance d'interface thermique optimale
US20130291555A1 (en) 2012-05-07 2013-11-07 Phononic Devices, Inc. Thermoelectric refrigeration system control scheme for high efficiency performance
FR3007114B1 (fr) * 2013-06-18 2015-07-17 Coldway Dispositif modulaire externe de regulation autonome de temperature d une enceinte
US9593871B2 (en) 2014-07-21 2017-03-14 Phononic Devices, Inc. Systems and methods for operating a thermoelectric module to increase efficiency
US10458683B2 (en) 2014-07-21 2019-10-29 Phononic, Inc. Systems and methods for mitigating heat rejection limitations of a thermoelectric module
CN105433819A (zh) * 2014-08-27 2016-03-30 上海合既得动氢机器有限公司 氢气烧烤炉
FR3026828B1 (fr) * 2014-10-01 2016-11-11 Coldway Procede de mise en temperature et de maintien en temperature de l'interieur d'une enceinte thermiquement isolee sans apport d'energie continu- dispositif associe
CN104990336B (zh) * 2015-06-15 2020-07-21 中国天辰工程有限公司 一种合成氯乙酸的高温冷却水***
CN106979146B (zh) * 2017-05-11 2019-09-24 王政玉 一种热动力增压泵
RU2745434C2 (ru) * 2019-07-31 2021-03-25 Сергей Леонидович Терентьев Абсорбционная холодильная машина

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FR2679633A1 (fr) * 1991-07-26 1993-01-29 Faiveley Sa Installation pour produire du froid par reaction solide/gaz, le reacteur comportant des moyens de refroidissement.

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US1954056A (en) * 1930-11-18 1934-04-10 Chester F Hockley Adsorber system
US2257735A (en) * 1937-01-22 1941-10-07 Kleen Nils Erland Af Absorption refrigerating system
US2276947A (en) * 1938-10-01 1942-03-17 Kleen Nils Erland Af Refrigerating apparatus
US2340886A (en) * 1940-06-13 1944-02-08 Kleen Refrigerator Inc Thermostat valve operating mechanism for absorption refrigerating apparatus
US2587996A (en) * 1943-07-05 1952-03-04 Hoover Co Absorption refrigeration
US2461262A (en) * 1945-06-02 1949-02-08 Kleen Refrigerator Inc Refrigeration
US2513148A (en) * 1946-08-22 1950-06-27 Hoover Co Intermittent absorption refrigeration
US2539986A (en) * 1948-01-16 1951-01-30 Hoover Co Cooling system for refrigerators
US4183227A (en) * 1977-01-17 1980-01-15 Exxon Research & Engineering Co. Heat pump
DE3509564A1 (de) * 1985-03-16 1986-09-18 Thomas Dipl.-Ing. 7500 Karlsruhe Föllinger Apparatur zur durchfuehrung von adsorption, desorption und innerem waermeaustausch
WO1992022776A1 (fr) * 1991-06-17 1992-12-23 Rocky Research Systeme continu et a pression constante ameliore, utilisant un agencement etage de composes vapeurs-solides
FR2679633A1 (fr) * 1991-07-26 1993-01-29 Faiveley Sa Installation pour produire du froid par reaction solide/gaz, le reacteur comportant des moyens de refroidissement.

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0702199A1 (fr) * 1994-09-19 1996-03-20 Nippondenso Co., Ltd. Appareil de refroidissement à adsorption
US5619866A (en) * 1994-09-19 1997-04-15 Nippondenso Co., Ltd. Adsorptive type refrigeration apparatus
WO1996030706A1 (fr) * 1995-03-28 1996-10-03 Rocky Research Systemes ameliores de chauffage et de climatisation utilisant des reacteurs de sorption a vapeur solide capables de taux de reaction eleves
CN102155813A (zh) * 2011-04-20 2011-08-17 上海交通大学 空调机组冷凝热驱动的热化学吸附制冷装置
US10006670B2 (en) 2013-05-02 2018-06-26 Carrier Corporation Method for managing a refrigerant charge in a multi-purpose HVAC system
US10240825B2 (en) 2013-11-13 2019-03-26 Mahle International Gmbh Evaporator set, preferably for a thermally driven adsorption device, and adsorption device
CN103615831A (zh) * 2013-11-15 2014-03-05 无锡雪浪环境科技股份有限公司 一种蒸汽压力升降吸附法及使用该方法的热泵
CN103615831B (zh) * 2013-11-15 2016-06-22 无锡雪浪环境科技股份有限公司 一种蒸汽压力升降吸附法及使用该方法的热泵
WO2017207262A1 (fr) * 2016-05-30 2017-12-07 Climatewell Ab Tube caloporteur hybride

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DE69420404D1 (de) 1999-10-07
KR960702597A (ko) 1996-04-27
BR9406573A (pt) 1996-01-30
HU9503185D0 (en) 1995-12-28
JP3391795B2 (ja) 2003-03-31
CN1099563C (zh) 2003-01-22
CA2160659C (fr) 2006-07-11
EP0697085A1 (fr) 1996-02-21
AU6709094A (en) 1994-12-12
SG47748A1 (en) 1998-04-17
HUT73008A (en) 1996-06-28
EP0697085B1 (fr) 1999-09-01
CZ285095A3 (en) 1996-08-14
HU219393B (en) 2001-03-28
CN1123053A (zh) 1996-05-22
RU2142101C1 (ru) 1999-11-27
DE69420404T2 (de) 2000-02-10
CA2160659A1 (fr) 1994-11-24
ATE184098T1 (de) 1999-09-15
KR100358338B1 (ko) 2003-03-03
ES2137365T3 (es) 1999-12-16
TW314584B (fr) 1997-09-01
JPH08510045A (ja) 1996-10-22

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